Method of producing coke and distillate



July 31, 1934. HESS 1,968,038

METHOD OF PRODUCING COKE AND DISTILLATE Filed Jan. 16, 1929 7 Streets-Sheet l I 317672- Z r: Ewan/5 .JW. Hess;

July 31, 1934.

F. M. HESS 3 METHOD OF PRODUCING COKE AND DISTILLATE 7 Sheets-Sheet 2 Filed Jan. 16, 1929 LUcfiZEY- Harlem M HESS,

July 31, 1934. i F. M. HESS METHOD OF PRODUCING COKE AND DISTILLATE 7 Sheets Sheet 3 Filed Jan. 16, 1929 5 m w I w Jilly 31, 1934.

F. M. HESS METHOD OF PRODUCING COKE AND DISTILLATE Filed Jan. 16, 1929 7 Sheets-Sheet 4 F. M. HESS 1,968,038

METHOD OF PRODUCING COKE AND DISTILLATE 7 Sheets-Sheet 5 July 31, 1934.

Filed Jan. 16, 1929 $206M nmobs J 1 fifss,

July 31, 1934.

M. HESS Filed Jan. 16, 1929 METHOD OF PRODUCING COKE AND DISTILLATE '7 Sheets-Sheet 7 25506183? Fez/7101 19 i 1113.15;

" 3 JMMWJ My fiatentecl July 31, 193 4 UNITED STATES METHOD OF PRODUCING COKE AND v DISTILLATE Francis M. Hess, Chicago, Ill.

Application January 16,

1929, Serial No. 332,841

11.01aims. (01. 262-6) According to the present invention; there is employed, for the production of coke on the one hand, and valuable distillate by-products such as gasoline'and benzol on the other, a mixture of.

powdered coal and a hydrocarbon liquid, such as crude petroleum, and this mixture is mechanically forced through one or more stills, and preferably also through a condenser and a dephlegmator on its way to the still or stills, and thence into a coking chamber in which the plastic residuum from the still or stills is mechanically formed into briquettes of uniform size which latter are subjected to further restricted combustion in the presence of steam and air; this highly heated steam and air together with the hot vapors and gases resulting from the restricted combustion fiowing countercurrent through the coking chamber, still or stills and dephlegmator (when used) and supplying the heat to efiect distillation, and merging and mixing with the distillate products, preferably in the presence of a catalyzing agent to facilitate cracking; the condensible fractions of the mixture being liquefied in the condenser, and the non-condensible or fixed gas portion flowing to a suitable receiver.

Among the objects of the invention are to produce an improved quality of coke, which 1' accomplish chiefly'through the employment of a much lower coking temperature than has heretofore been employed in coking operations; to' produce a coke well suited to customers demands,

to accomplish the production of the coke without waste or the accompaniment of any coke breeze,

Many other objects and attendant advantages of the invention will become apparent to persons skilled in the art as the same becomes better understood by reference to the following detailed description, taken in connection with the accompanying drawings illustrating an apparatus embodying the principle of the invention, in which- Fig. 1 is a partly diagrammatic elevation of the complete plant, with the mixing tank shown in vertical axial section; Fig. 2 is a horizontal section through the lower portion of the mixing tank, taken on the line 2-2 of. Fig. 1; I

Fig. 3 is a vertical section through the condenser and the dephlegmator and their connecting pipes; Fig. 4 is a vertical section through one of the dephlegmator tubes;

Fig. 5 is a vertical longitudinal section through a portion of the upper and lower still sections and the throat connecting said sections;

Fig. 6 is a horizontal section taken on the line- 6-6 of Fig. 5;

the upper still section taken on the line '7-7 of Fig. 5;

Fig. 8 is a vertical longitudinal section through the receiving end of the upper still section, the lower end of the dephlegmator, and the throat between said parts;

Fig. 9 is a transverse section taken on the line 9- -9 of Fig. 8;

Fig. 10 is an enlarged elevation of the coking chamber and the discharge end of the lower still section, also showing in section the motors which operate the coking plunger and the coke discharge plunger and valve, and in elevation the valve-actuating mechanism of said motors;

Figs. 11 and 12 are details in side elevation of parts of the one-way valve-actuating mechanism;

Fig. 18 is an enlarged vertical axial section through the coking chamber and the discharge end of the lower still section, showing the moving parts in the coking chamber in fully raised position;

Fig. 14 is a vertical section through the bottom wall of the coking chamber, showing one of the, coke discharge openings and cutters and air and steam distributors cooperating therewith;

Fig. 15 is a detail in side elevation of a portion of the coke plunger stem with a cam groove therein for oscillating the cutter across the coke dis charge opening;

Fig. 16 is a section detail on the line 16-16 of Fig. 13;

Fig; l? is a view similar to Fig. 13, taken in a. plane at right angles to the sectional plane, of Fig. 13;

Fig..i8 is a top plan of one of the removable catalyzer cartridges, in horizontal section through its containing tube;

Fig. 19 is a vertical section through a portion of one of the catalyzer cartridges;

1 Fig. 2G is a detail section of a coupling member between the yoke of the coking plunger and the cover plate of the vapor discharge flue which contains the catalyzer cartridges, taken on the line 2020 of Fig. 17.

General organization pulverized coal is thoroughly mixed with a liquid hydrocarbon; B designates as an entirety a condenser through Which the mixture is forced by a pump in an upward direction, and through which-vapors evolved in the still are caused to flow in a downward direction, imparting their heat to the mixture; C designates as an entirety a dephlegmator preferably located alongside of and communicating with the condenser, through which the mixture flows in a downward direction and the vapors from thestill flow in. an upward direction; D and D are upper and lower sections, respectively, of the still through which the mixture flows successively in thin films over heating plates in a downward direction, and through which vapors from the coking chamber flow upward; and E designates as an entirety a coking chamber in which the residuum from the still is;

highly heated, formed into short cylindrical sections or briquettes, subjected to further combustion by a blast of mingled steam and air in the presence of a high temperature to drive offremaining volatile constituents, and finally delivered into a quenching chamber and discharged from the latter.

Mixing tank Referring to Fig. l, the mixing tank A consists of a cylindrical shell 1 having a conical bottom 2 terminating in an outlet T The-bottom of the T 3 is equipped with a packing gland 4 through which and the shell 1 passes a vertical shaft 5. The lower end of shaft 5 carries a pulley 6 which maybe driven by any suitable source of power. Fast on the shaft 5 within the conical lower portion 2 of the tank are paddles 7. Above the mixing tank 1 is a cylindrical shell 8 formed with a lower reduced cylindrical neck portion 9 mounted in the top wall ofthe tank 1. In the top wall of the shell 8 are a pair of hinged downwardly opening doors 10 directly underlying a feed chute 11 through which the powdered coal is delivered. Fast on the shaft 5 within the neck 9 is a feed screw or spiral l2, and above the latter are a pair or" feed paddles 13 directly beneath a conical spreader 14. The neck- 9 ofthe shell 8 extends downwardly into the mixing tank 1 to a point normally below the level of the liquid in the latter to form a seal. Tank shell 1 is equipped above the seal line with a pipe 1. controlled by avalve 1 to allow moisture carried-by the coal'to escape.

The stem of the T- 3 is connected into a pipe 15 leading into the suction side of a rotary pump 16, the pipe 15 being equipped with'valves 17 and 18. Communicating with the pipe 15 between the valves 17 and 18 is a pipe 19 through which the hydrocarbon liquid, which may be either coal tar or petroleum or one of their high boiling distillates or reflux from a previous run, is suppliedwhen first starting the system in operation, pipe 19 being equipped with a valve 20; valves 17, 18 and being at that time open. From the discharge side of the pump 16 a pipe line 21 equipped with a pressure-controlling valve 21' leads into the condenser E, and from the pipe line 21 is a branch pipe 22 which extends through the top of the mixing tank 1. and is supplied with a relief valve 23 normally held closed by a weight 24 and, below the relief valve, with a normally open valve 25 adapted to be closed by a float 26'when the level of the liquid. in-the-mixing tank rises above a predetermined height.

The condenser ing from the. discharge side of the pumplfi is extended through the side wall of the lower chamber 34 and at its upper end is connected into the lower partition plate 31. The mingled coal and oil pumped, upwardly through pipe 21 fills the intermediate chamber 33 around the tubes 35 and flows thence through an outlet pipe 36 over into thedephlegmator. The purpose of the intermediate chamber 33 and its tubes 35 is to provide a heat exchange between the hot down-flowing vapors and the cold up-fiowing mixture on its way to thevstill. Connected into the lower tank head 29 is a discharge pipe 37 which leads, through a level. fixing device indicated at 38 in Fig. 1, to a receiving tank 39 for the condensate which latter may be drawn ofi through a pipe 40 equipped with a valve 41. Entering the upper end; of tank 39 is a pipe 39' equipped with a hand valve 39.

for regulating pressure in the system through release of gas produced. For a. description of the leveling device 38 reference may be-had to Letters Patent No. 1,610,523, granted to'me on the 14th day of December, 1926. i

The dephlegmator the upper chambers 32 and 48 of the condenserand dephlegmator, and extends thence down.- wardly through the-partition. and chamber 49 centrally of the. latter. The lower end of pipe 36,

is closed and terminates a short distance above the parition 46; and the portion of the pipe 36 lying between the partitions 45 and 46 is provided with a plurality of spaced apertures 52 through which the material undergoing treat:- ment trickles into the intermediatechamber 49; building up in the latter to an extent permitted by a regulating valve 53in a pipe 54 that communicates through the lower partition plate 46 with the bottom of the intermediate chamber 49;

passed to the upper section 13 of the still. Just below the lower partition plate so is an annular apron- 56 formed with downwardly and 1 inwardly;

tapered walls by which reflux from the dephlegmator is directed into a pan57 mounted in the chamber 50 and provided. with a reflux return pipe- 58 passing through the side wall of: the

dephlegmator and extending thence into the suction pipe 15 ofthe pump (Fig. 1) between the valves 17 and 18.- Inthe pipe 58 is arelief-valve 59 held closed by a weight 60 and also a manually operated-valve 61. The portion of the reflux that overflows pan 57 mixes with feed material from,

pipe 54 and the two together pass through the neck 55 into the still. The dephlegmator tubes 47 preferably contain removable perforated tubes 62, one of which is shown in Fig. 4, which tubes 62 are filled through their open tops with catalyzing contact bodies to aid cracking, the lower ends of the tubes 62 being perforated to pass the vapors flowing upwardly from the still through the lower chamber 50. ofv the dephlegmator.

the sections.

eas es The still" The structural details of the upper section D of the still are shown mainly in Figs. 5 to 9 inclusive. Said upper section comprises a circular shell or drum 63 inclined downwardly from the dephlegrnator and closed at its ends by tank,

heads 64 and 65. In the bottom of the tank 63 is laid a segment trackway 66 for a purpose hereinafter described. Within and extending lengthwise of the drum 68 is a heating structure adapted to provide for the multiple downflow of the material to be distilled and coked and also the up and down flow of heated gases from the coking chamber supplying heat to the material undergoing distillation. In the structure shown a group of three superposed liquid and gaseous flow devices is shown. 67, 67 and 67 designate upper, intermediate and lower flow plates, and

68, 68 and 68 designate corresponding plates 79 and 71 for the upfiow of hot gases from the coking chamber. Within the passages 69, 70 and 71 are preferably placed corrugatedsteelplates 72 forming supports for the plates 67, 67 and 67 Above the flow plates 67, 67 and 67' are hollow,

screens 73 that are filled with catalyzing contact bodies; and underlying the plates 68, 68 and 68* are similar hollow screens 74 containing contact bodies. The intermediate and lower screens 73 may be formed continuous at their longitudinal edges with the upper and intermediate screens 74, as shown in Fig. 7. Extending through each of the screens 74 is a series of perforated pipes 75, the up er ends of which, as shown in Fig. 8,

communicate through the plates 68, 68 and 68 with the conduits 69, 79 and 71, whereby the hot gases flowing upwardly through said conduits return in the reverse direction through the pipes 75, the gases being diifused through said perforated pipes and the catalyzing contact bodies in the screens 74. From the lower ends of the flow plates 67, 67 and 67 thematerial drops into the lower end of the drum 63 and flows thence into the high end of the underlying still section D in the manner hereinafter described. i

Extending transversely through the lower ends of the flow plates and gas conduits above de scribed is a tubular sectional manifold comprising flanged sections 76, 76'; 77, 77', and 78, 78, the spaced circular flanges of each pair being welded or otherwise secured to the flow plate and its underlying conduit bottom plate, which plates, as shown in Fig. 5, are connected at their lower ends by a closure strip 79, having a hollow tongue 79 interfitted between them andv abutting at their centers against the flanges of The upper end or" the manifold is closed by a cover plate 80, and the lower end of the manifold is attached to a tube 81 of the same diameter that connects the same with a corresponding manifold in the lower still section D. By the construction above described, upfiowing hot gases from the lower still section pass freely into the heating conduits 69, 70 and 71, and return through the perforated pipes 75. It will be noted from Fig. 5 that the pipes and the screens in which said pipes are contained terminate short of the manifold so that the return gases pass freely to the interior of the drum 63.

'Themultiple flow structure hereinabove described is'embraced and held together by a plurality "of U-shaped channel bars 82, to the lower ends of which." are secured depending brackets 83 in and between which is journaled an axle 84 equipped with wheels 85 resting on the trackway 66, so that the structure may automatically accommodate itself to longitudinal expansion and contraction without strain.

, Referring to Figs. 8 and 9, the material to be distilled flowsfrom the, lowermost chamber 50 of the dephlegmator through the tubular neck 55 and, thence through an opening 86 in the top of the drum 63 and a spout 87 communicating with said openinginto a distributing trough 88 that extends crosswise of and above the upper heating plate 67. From the trough 88 the material is distributed through pipes 89, 96 and 91 to overflow troughs 92, 92 and 92 directly overlying, the uper ends of the heating plates 67, 67 and 67 respectively, whereby the material is uniformlyand. simultaneously distributed to said heating plates. Extending coaxially through the neck 55 is an upflow pipe 93 (Fig. 8) through whichth'evapors and gases flow from the drum 63 upwardly into the dephlegniator.

The lower still'section D is substantially a duplicate-of the upper still section D, but is inclined in the reverse direction to continue the gravity flow oi the stock undergoing treatment, and omits the screens 74 of the upperstill section and the pipes 75. The lower still section is connected'to the upper section by a hollow neck 94, within which latteris a tubular member 95 open at, its upper and lower ends to the interiors of the upper and lower still sections respectively. The lower end of the tubular niember 95 is formed with an annular flange 96, be-

tween which and the upper wall of the lower still drum 97 is interposed an annular gasket 98 to seal the lower end of the annular flow passage between the neck 94 and the tubular member 95. In the lower still section is a sectional manifold designated as an entirety by 99 which is structurally identical with the sectional manifoldpreviously described in connection with theupper still section, the two manifolds being joined by an intermediate connecting manifold 10-9 extending through the tubular member 95 and spaced from the latter by lugs 199 thereon, thus providing an annular flow passage 191 for vapors distilled in the lower still section up into the upper still section. In the flange 96 is a discharge opening 102 communicating with a spout 103 that delivers to a distributing trough 10 structurally identical with the distributing trough 88 of the upper still section; and connected into the bottom of the trough 194 are pipes 105,106 and 107 that conduct the stock into overflow troughs 108, 108' and 108 that overlie the upper ends of heating plates 109, 109 and 109 respectively. These heating plates are mounted and supported in the same manner and by the same means as the heating plates 67; 67 and 67 'of the upper still section and are covered by screens 116 corresponding to the screens 73 of-the upper still section.

As best shownin Figs. 10, 13 and 17, the lower end of the lower still drum 97 merges into a vertical cylinder 111 surmounting the cokin'g chamber, and closed'at itsupper end by a head 112.

Coking. apparatus The coking mechanism isshown principally in. Figs. 13' to 20 inclusive. Continuous with the lower end of cylinder 111 is a cylinder 113- of greater diameter having. an internal; lining. 114

of refractory material and. forming a coking chamber 115, and a cup-shapedv bottom 116 that provides a, quenching chamber 117,. l'he sides of the coking chamber 115 are, provided with manholes and manhole covers. 118, and the quenching chamber 117 has a bottom delivery flue 119 (Fig. 10) that communicates with. a power operated discharge mechanism hereinafter described. The coking chamber 115 has a bottom wall or floor 120, and a transverse partition 121 some distance above the floor. Extending transversely through and depending from the lower ends of the flow plates and gas conduits oi the lower still section D is. a vertical gas flue,

or manifold 122, the upper portion of which has.

which reciprocates a piston 125 the piston-rod.

126 of which extends downwardly through a stuffing-box 127 on the cylinder head. 112. and is connected to a vertical yoke within the cylinder 111. The depending limbs of yoke 128 pass through holes in the roof of housing123,,as shown in Fig. 1'7, and at their lower ends are connected to a circular plate 129. that is centrally apertured, to accommodate the manifold 122. Depending from the plate 129 is a sleeve 130, the lower portion of which is perforated as shown at 130' for a purpose hereinafter described. Continuous with the lower end of sleeve 130. is a hollow extension member 131. that slides through a. bearing boss 120 on the floor plate 120. and has longitudinal grooves 132 in its sides engaged with lugs 133 on the boss. 120 to prevent turning movement of member 131. The lower portions of the grooves 132: are inclined, to form cams 132 (Fig. 15), which actuate a cutter hereinafter described. Depending from member 131 is. a plunger 133 which forces the severed and quenched coke cylinders into and through the delivery flue 1'19.

Encircling and slidable over the sleeve 130 below the plate 129, is another disc or plate 134, and between the plates 129 and 134 is a circular group of compression springs 135 normally urging said plates apart; and similarly encircling and slidable over the sleeve 130- below the plate 134 a plunger plate 136 carrying on its under side a circular group of plungers 13'1. The plate 136 is normally upheld by a group of thrust springs 138 against stops 140 on the inner wall of the housing 123', said springs 138 being footed on a fourth disc or plate 141 surrounding andsl-idahle on sleeve 130 and normally upheld by latch springs 142 attached to the inner wall of housing 123. On the under side of plate 141 are lugs 141 adapted to strike the bottom plate of housing 123. On the under side of the bottom wall of hous ing 123 is a circular group of laterally apertured tubes 143 that extend through thetransverse wall 121 and into which the hot semi-viscous residuum in the coking chamber flows and through which it is forced by the plungers- 137. On the under side of plate 141 is a circular group of tubular scrapers144that reciprocate through and scrape the internal walls of the tubes and encircle the plungersv 137. Depending from plate 134. is a, circular group of tubes 145v having centrally apertures] lower end walls and annular shoulders 145 that are movable through holes 135' in plunger plate 136; and on the upper side of plate 141 is a circular group of tubes 14-6 having centrally apertured top walls. Between the plate 1'41 and the shoulders 145." and centered on the tubes 1'45 and 146', is a, circular group of compression springs 147, and extending through the bottom walls of tubes 145 and the top walls of tubes 146: are rods 148 having headed ends that serve to limit the extent of separation of plates 134 and 141 under the thrust of springs 147;

In the chamber between the transverse wall 121 and the bottom wall 120 is a circular group of hollow columns 150 made of refractory material and having embedded therein a series of electric heating rings 151 placed one below another and of increasing heat intensity from top to bottom. so that as the coke cylinder passes downwardly through the column it encounters an increasing temperature zone. The columns 1'55 are also perforated laterally, as shown at 150', to permit escape of gases from the coke cylinders to the chamber surrounding the columns. Between the tops of the columns 15c and the under side of the wall 121 are preferably interposed one or more plates 152- forrned with conical holes 152 that register with the lower open ends of the tubes 143 and cause the successive cylinders of semi-plastic coke forced downwardly bythe plungers 137 to hang suspended from plate 152, the successive cylinders sticking to each other. In the bottom wall 120 are discharge openings 153 registering with the lower ends of columns 150, and below the bottom wall 120' are a pair of plates 154 and 155 formed with conical holes 154 and 155 therein, both registering with the openings 153. In th plate 154 are radial ducts 156 leading outwardly from the openings 154* to a circumferential duct 157, and inthe plate 155 are similar radial ducts 158 leading outwardly from the openings 155' and communicating at their outer ends with the ducts 156. Communicating with the circumferential duct 157 is a T-union 159 into which are connected a steam pipe 155 having a throttle valve 16-1 and a compressed air pipe 162 having a throttle valve 163. By this means compressed air, or a graduated mixture of compressed air and steam, is admitted to the coking chamber through the perforated hollow columns 156 to control restricted combustion.

Below: plate- 155 is a cutter disk 164 supported at its outer periphery on ball bearings 165. In this disk are conical openings 166 movable into and out of register with the openings 155 when the disk is oscillated, the upper edges of the openings 166 acting as cutters to shear off a depend ing column of coke. The cutter disk is oscillated by the rising and falling movements of the extension member 131 by lugs- 167 on the hub of the cutter disk engaged with the cam grooves 132" of the member 131.

In the quenching chamber 117 is mounted a ring 168 connected to a water supply pipe and apertured on its. lower side to direct jets of water onto the coke columns as they fall into the quenching chamber.

With a view to recovering from the coking op- 159 eration the highest possible amount of valuable distillate by-products I preferably employ in the vertical gas flue or manifold 122 a stack of erforated containers 170, forming in effect a sectional scrubber screen, and shown in detail in Figs. 18 and 19. These containers carry catalytic contact bodies that serve as cracking agents. To facilitate application and removal the containers 170 are equipped in their side walls with rollare 171 that ride in grooves 172 in the wall of the flue column 122; Internal lugs 173 at the bottom of flue 122 form stops for a perforated plate 174 on which the lowermost container rests. Means for removing the containers when required to renew the contact bodies consists of the following. Resting on top of the flue 122 is a plate 175, through which extend vertical strips 176, in the lower end of which are mounted pulleys 177. Over these pulleys pass two cables 178 joined at their upper ends at 179; these cables extending downwardly between the stack of containers 170 and the flue 122, and at their lower ends attached to the plate 174. The length of the cables is preferably so adjusted that when the screen sections or containers are fully lowered to operating position the plate 1'74 will be slightly above and out of contact with the lugs 173, so that the weight of the stack is eifective to hold plate 175 in gas-tight contact with the top of flue 122. If, however, a cable should stretch or break, the stop lugs 173 prevent the stack from dropping through the lower end of the flue. The upper ends of lugs 176 (see Fig. 13) are apertured, and to the cross-bar of the yoke 128 are attached a .pairof clips 180 having apertured depending portions 180 (see Fig. 20) that, when the yoke 128 is in its fully lowered position, straddle the lugs 1'76, so that coupling pins may be entered; and on the next rise of the yoke 128 the stack of containers is raised suiflciently to bring the topmost one out of the flue 122. Access is had to the containers through a large manhole opening 181 equipped with a cover 182 in the side of cylinder 111, and when the topmost container has been .removed, the others may be successively removed by gradually raising the cables 178 by hand.

, In the bottom of the sleeve 130 is mounted a conical deflector 183 by which the reflux from the flue 122 is directed back into the coking chamber.

Referring to Fig. 10, it will be seen that the delivery flue 119 of the quenching chamber communicates with the upper side of a horizontal cylinder 184 that forms an element of a coke discharging mechanism that is so constructed as to seal the interior of the system against loss of pressure, and is actuated in proper synchronism with the coke forming apparatus actuated by the overhead cylinder 124. Reciprocable in the cylinder 184 are tandem plungers 185 and 186 connected and spaced by a piston rod 187. Communicating with the lower side of cylinder 184 and laterally ofiset from the delivery flue 119 by the length of plunger 186 is a discharge pipe or flue 188. Piston rod-187 is actuated by a piston 189 in horizontal cylinder 190. Steam or compressed air is supplied to the-valvechest 191 of cylinder 190 by a main supply pipe 192 equipped with a hand cut-ofi valve 193, and to the valve chest 194 Assuming that the parts are in the positions shown in Fig. 10 with valve 193 and 196 open, steam enters the top of cylinder 124 forcing down piston 125 and causing plunger 133 to deliver a measured charge of coke cylinders or briquettes through delivery flue 119 into the space between the plungers 185 and 186 (the description of the operation of the moving parts inside the coking chamber being reserved to the description of the operation of the complete system). As piston 125 approaches the limit of its down stroke, a striker lug 199 on piston rod 126 strikes the horizontal arm of a bell-crank lever 200 and, through link 20]., bell-crank 202, link 203, bell-crank 204, and valve-rod 205, shifts valve 198 to admit steam to the right hand end of cylinder 190 and exhaust steam from the left hand end. It will be observed by reference toFig. 11 that the horizontal arm of bell-crank 200 is jointed, so that the striker lug 199 on its return or rising movement merely trips the arm idly. Piston 189 then travels to the left, causing plunger 185 to carry the charge of coke to the mouth of discharge flue 188, through which it falls. As piston 189 starts on its working stroke, a striker lug 206 on piston rod 187 at first idly trips the jointed depending arm of a bell-crank 207 (see Fig. 12), and near the limit of its working stroke rocks a pivoted lever 208 which, through bell-crank 204 and valve rod 205, reverses valve 198 and admits steam to the left hand end of cylinder 190.: This rocking of bell-crank 204 at thev the limit of its return or idle stroke, the striker lug 206, through bell-crank 207, link 209, bellcrank 210, link 211, bell-crank 212, and valve-rod 213, shifts slide valve 197 to a position to admit steam beneath piston 125 thereby efiecting the rising movement of the latter and plunger 133. As piston 125 approaches the limit of its upward travel striker lug 199 rocks a pivoted lever 214 which, through bell-crank 212 and valve-rod 213, reverses valve197 and admits steam to the top of cylinder 124. This rockingof bell-crank 212 at the same time restores bell-crank 207 to the position shown in Fig. 10. It will thus be seen that the complete cycle comprises, first a down or working stroke of piston 125, then a left-hand or working stroke of piston 189, then a right-hand i or return stroke of piston 189, and thenan up or return stroke of piston 125. V

In the chamber containing the columns may be located a thermocouple 220 to automatically cut the electric heating rings 151 into and out of circuit to maintain the desired temperature in said chamber, which temperature is normally regulated by the steam and air introduced through pipes and 162.

The regulating valve 53 and pressure-control- -ling valve 21 may be operated from a distance by any suitable operating connections, such as are conventionally shown in Fig. 1 as consisting of suitably 'journaled vertical and horizontal rods connected by mating miter gears, the system controlling valve 53 being actuated by a hand Wheel 221, and that controlling valve 21 by a hand wheel 222.

. Operation Assuming that the apparatus has been out of service and is just starting up, the entire system is first purged with steam to be sure all air is expelled. Then a slow feed of liquid is started through valve 20, and valves 17 and 18 are opened. Thisliquid may be either coal tar or petroleum, or one of their high boiling distillates or reflux from a previous run. Valve 21" is then opened by hand wheel 222 andpump 16 is started. As weight 24 on relief valve 23 will not allow valve 23 to open until pressure on lines 21 and 22 is somewhat higher than the system will be operating under, no liquid will pass here unless valve 21 is nearly enough closed to allow pump 16 to build a pressure upon the line 21 sufiicient to open valve 23.

This liquid fills middle chamber 33 of condenser E and flows over into middle chamber 49 of dephlegmator C.. The latter chamber is allowed to fill about half full before opening valve 53 by hand wheel 221. With valve 53 finally open the liquid flows down through line 54, chamber 50, neck 55, spout 87, distributing trough 88, pipes 89, 90, 91 over overflow troughs 92, 92 and 92 and onto plates 67, 6'7 and 67 of the upper still section D. I

The liquid feed. continues down over the heating plates of stills D and D and finally flows into compartment 115 of coking chamber E. With all of plungers 137 in a raised position the hydrocarbon liquid trickles down through perforated tubes 143 over the internal walls of columns 150 containing heating rings 151. With the current turned on the latter, the temperature of this zone is quickly raised to redness and the hydrocarbon liquid is vaporized and gasified in trickling down said columns. The vapors and gas pass up through perforated plate 174 and up through scrubber screens 170. They continue up to and through heating plates of still I) and D and shortly a distillation temperature is reached in both stills. The vapors from within the plates finally issue through openings in pipes '75 and mix with the vapors evolved in the still. Together these pass up through upfiow pipe 93 and up through the perforated contact tubes within the dephlegmator tubes 47. As the liquid feed has already built up in depth around each tube refluxing starts immediately and drops down on deflecting apron 56 and into pan 57. Valve 59 is held closed by weight 60 and the reflux liquid builds up and overflows pan 57. The scrubbed. vapors and gas pass over through pipe 51 and the vapor is condensed in passing through the tubes 35 in the condenser. The leveling device 38 can be adjusted to maintain any height of liquid distillate in the condenser tubes. Finally the liquid hydrocarbon distillate and the permanent gas flow down through pipe line 37 into receiving drum 39. With valve 39 open, the permanent gas passes through to any outside storage. The distillate may also be drawn ofif through valve 41 to any convenient receptacle.

This slow distillation is continued until the entire apparatus reaches a desirable temperature and then valve 39 is closed. The apparatus will now build up to the desired operating pressure very rapidly and the temperature will. came up accordingly. The desired pressure from this point on is maintained by careful manipu1ation of valve 39 As soon as the desired pres sure is reached on the system valve 59 will open as re weight 60 will be overcome by the operating pressure plus the weight or column of reflux between valve 59 and pan. 57. Weight 60 is so adjusted that line 58 will be more than full at all times. This prevents gas or vapor being lost to the system at this point and keeps all vapor from passing to the mix tank as such. At the same time all of the reflux may be per mitted to get to the mix tank or only a portionas desired by partly closing valve 61.

It is now time to allow a mixture of air and steam to enter coking chamber E through valves 153 and 161. Restricted combustion starts immediately. From then on the electric rings only act as an emergency heat. In case anything happens to the air or an excess of steam issues from line 160 the electric elements 151 are automatically cut in circuit due to the temperaturecontrol exerted by thermocouple 220 inserted into the path (it the hot gas and vapor leaving the coking chamber. As soon the temperature is brought back to normal either by the eifect of the electric elements or the readjustments of air supply orboth, the current is shut off from the elements in the same manner that it was first turned on. As a further means of automatic control a thermocouple 220' (Fig. 17) may be added in the path of flow of residuum dropping from still D to coking chamber 115. This would operate in conjunction with thermocouple 220 and would maintain a shorter range of tempera.- ture at all times. The function of this type of control is old in the art and need not be discussed here.

The rate of the liquid feed passing valve 20 is now increased until it reaches the rated capacity of the apparatus. It is now time to start adding powdered coal through doors 10. This coal drops down on cone 14 in chamber 8 and is spread around the entire cylinder. Pulley 6 is set in motion, and in turn shaft .5 mixing paddles 7 and spiral feed 12 are also set in motion. The feed of powdered coal is gradually increased until it is brought up to the rated capacity of the apparatus. If any outside liquid is to be added, it is still admitted through valve 20 at the rated percentage decided upon. If not, valve 20 is now closed and the mix tank will depend on reflux for its liquid. Then, to get the best results, the feed mix is carried as high as possible in middle chamber 49 of the dephlegmator and still produce the desired fraction of cracked distillate through pipe 51. The object of course is to get the largest percentage of reflux to the mix tank. This in turn will bring the percentage of powdered coal in the final mix that passes valve 21" low enough to avoid settling out, and allow the reflux con tent to later wash the heating plates free from dirt and adhering particles.

The cycle of the mix tank is as follows. -The paddling effect'is sufficient to get the coal in solution or at least to hold the small particles in suspension. To facilitate this the hot reflux is irnmediately let down to the mix tank and its heat will not only affect the coal better in producing a hot solution, but it will also raise the temperature high enough so that all the water content of the coalwillbe vaporized and then allowed to escape as such through pipe 1' and valve 1 to any convenient outside disposal. Additional mixing is accomplished by the pump. A centrifugal pump is preferable. The pump should have a much higher rated capacity than is required for feed through 1 .v.

valve 21'. With this arrangement a more even feed pressure can be maintained at valve 21 and the bulk of the excess can be diverted back to the mixing chamber 1 by careful manipulation of weight 24 on weighted valve 23. This excess will I" would indicate that the rate of coal feed was too great. It is to be .noted that reflux from line 58 goes to the suction side of the pump first. This is an additional precaution to be sure that the feed mix finally passing valve 21' is lean enough at all times to avoid settling out and also that no slug of coal that is not properly mixed will get as far as valve 21. To further facilitate holding a desirable level in the mix tank two test cocks 223 and 224 may be employed. Theupper cock 223 would indicate to the operator that the level is too high if the liquid escapes when this cock is opened. The lower cock 224 would indicate that the level is too low if gas escapes when thiscock is opened. The desirable level is a point as close to the upper cock 223 as is possible for the operator to maintain.

' Soon after the powdered coal has been admitted to the mix tank, the coke forming and feeding devices and their operating mechanism are set in motion. These function as follows. Steam or gas may be used as the fluid pressure medium. As cylinders 124 and 196 have a. larger diameter than the plungers 133, 185 and 186, they will develop ample power to operate the entire devices on the release gas from receiving drum 39 if it is desired to use this. In either event, the fluid pressure medium is admitted through valves 193 and 196. From then on the operation is automatic-thuspiston rod 126 starts downward as gas pressure develops above piston 125 in power cylinder 124. This in turn carries depending limbs of yoke 128 downward.

Lirnbs of yoke 128' in turn start plates 129 and 134 downward with not enough resistance to compress springs 135. Plate 134 continues downward and through shouldered tubes 145 and springs 147 forces plate 141 down in like manner. Plate 141 carries tubular scrapers 144 down to a point close to the outlet of tubes 143. Finally stop lugs 141' come in contact with the bottom wall of housing 123. This arrests movement of plate 141 and springs 147 then start to compress. The object of the movement so far has been to allow scrapers 144 to scrape the inside surface'of tubes 143 free from clinging particles, and at the same time to confine within the tubular scraper the portion of residue that has passed the openings in tubes 143 while the scrapers 144 were in a raised position. As the movement continuessprings 147 are compressed'until plate 134 is against plate 136 and then the'thrust of plate 134 against plate 136 carries the latter together with plungers 137 downward. The thrust of outer periphery of plate. 136 against the protruding surfaces of latch springs 142 presses the latter outwardly and allows plate 136 to pass them. 'This second step in the downward movement is to en-v able plungers 137 to force the confined segment of residuum ahead of them the knife edge openings 152' of plates 152. This residuum has tarried long enough in tubes 1,43 in'close proximity to the hot refractory wall 121 to be fast approaching a firm solid state. ,Plate 134 stops when springs 147 are compressed to the 'point where the tubes 145 strike the tops of tubes 146. Plate 136 and plungers 137 of course stop at the same time; Limbs of yoke 128 now continue in the third step of the downward movement and as plate 134 is at the end of its move- :hent springs 135 are compressed;

The location of grooves 132 is suchthat by the time movement of platev 1344s stopped,

the movement of yoke 128 will have carried said grooves 132' down so that lugs 167 on cutter disc w 164 engage grooves 132' and a circular motion of downwardly through cutter disc 164 results. This circular movement of disc 164 is facilitated by ball bearings 165 on which discs 164 is resting. Ihis circular movement is suflicient to carry openings 166 out of register with openings 155. This in turn severe the coke cylinders that are protruding through the openings 155 as a result of the downward movement of plungers 137.

In the meantime yoke 128 has moved plunger 133 down into delivery flue 119 which seals the latter against escape of internal pressure. Thus the several coke cylinders are held for the time being in chamber 117. While lying here they are continually being sprayed with water from perforated water pipe 168. The interval between the downward and upward movements of pistonrod 126 can be regulated by the rate of flow of gas through valve 193 to suit the coke quenching in chamber 117.

As the upward movement of yoke 128 begins, grooves 132 and lugs 167 move disc 164 back to its former position, that is, openings 166 are in register with openings 155'. While this is taking place springs 135 are being released. When springs 135 are released plate 134 starts upward as springs 147 expand. By the time springs 147 have fully expanded, headed ends of rods 148 will have engaged the top wall of tubes 146 and the bottom wall of tubes 145. Inus plate 141 will be lifted, but as latch springs 142 are holding plate 136, the latter cannot be raised. As a re sult plates 136 and 141 will compress springs 138. The object for doing this is to allow knife edges of plungers 137 to thoroughly clean the inside surface of scrapers 144 as 144 move upward and 137 remain stationary.

As plate 141 nears its former position, it is forced past the protruding lower surfaces of latch springs 142. This moves latch springs outward far enough to disengage plate 136 and the latter returns to its former position as springs 138 are thus released and expand. As plate 141 continues to rise latches 142 spring inward to normal position so that when plate 134 starts downward again plate 136 will be held as before.

Of course when the coal is first added at doors 10 there will be no coke formed in the coking chamber and there cannot be any until enough coal has worked its way to the coking chamber to create a substantial coke cylinder in tubes 143. Until that time all material passing the plates 152 will be vaporized or burned to ash.

When plunger 133 is raised from delivery fine 119 the coke in chamber 117 drops into 119 along with the spray of water that is continually coming from line 168. Thus the coke is thoroughly quenched and cooled. The steam evolved from this quenching finds its way up through the passageways 153 and is superheated and dissociated in the coking zones. As soon as plunger 133 returns to delivery fiue 119, on the next downward stroke, the gas back of piston 189 in cylinder 198 starts piston rod 187 moving to the left and as a result plunger 186 moves over beyond discharge pipe 188, 185 moves over between 119 and 133 and the space between the two plungers is brought directly over discharge pipe 188. As the coke has been pushed over with the movement'of these two plungers, the moment it gets to discharge pipe 188 it is released from the system, and on the return movement of pistons 185, 186 and 189 they are brought back to their original position.

As stated before, the bell-cranks function so that piston 189 makes both left and right strokes while piston 125 is at rest after its downward mote cracking.

movement. This of course is done to cause the least pressure loss to the system. As an addi tional precaution, steam may be automatically introduced into cylinder 184 through valve-con .3 trolled pipe 119, while piston 189 is making its two strokes.

The liquid used in the mix tank serves a variety of purposes. First the powdered coal is held in suspension. Later the liquid acts as the vehicle to carry the powdered coal through the condenser and dephlcgmator extract a large quantity of heat from both, Finally the mass isspread out over the several heating plates to accomplish low temperature distillation and cracking under pressure. Even at this point the liquid washes the inclined plates free from adheringparticles.

The reflux alone may be used to accomplish this washing. Thus the reflux revolving a desirable cycle that is particularly advantageous for desirable cracking. In rotating in this cycle the reflux is periodically vaporized an infinite number of times and each time it is vaporized its boiling point is cracked to a lower level, and at the same time a portion of the vaporized coal is carried with it.

On the other if it is so desired to mix petroleum or its distillates or other tars (as coal tar or water gas tar) with the reflux in the mix tank, this can be done and not disturb the existing reactions and thus serve as an additional flexibility in operation, because the outside liquid=can be mixed in any percentage desired to meet the ever changing requirements on the quality and texture the coke produced.

With the spiral feed arrangement in the mix tank this equipment can be resorted to as a sole means of maintaining a desired feed rate of coal into the system, if so desired, by merely changing the rate of travel of the mixing vanes. The pump automatically acquires maximum circulation and at the same time constant feed pressure. The relief valve operates in conjunction with this feature to prevent excessive pressures in the feed at any time. An additional feature to coordinate with this mixing is the trip valve 59 in the reflux line which permits all of the reflux to gain'access to the feed pump but at the same time does not allow any vapor from the still to pass it. The hot reflux with a partially cracked distillate content, is the best solvent for the coal well as a proficient dilutent for the insoluble portion, and vehicle to carry the entire to and over the heating plates. Thus dust and screenings are raised to equal value for feed as compared with any higher graded coal.

Circulating the reflux in a closed cycle allows the reflux to act in a triple capacity.- a) First it acts as a solvent for low volatile products in the coal (1)) second, it either holds the balance in a colloidal state or dilutes the mix to act as a v hicle, whichever case may be (depending on the structure of coal at hand) (c) thirdly,the reflux gets back to the still and serves its original purpose, without being hampered by the above duties exac ed, namely-40 afford favorable association of reflux that is partially cracked to raw material that is undergoing its original distillation under pressure. is accomplished of course because the two are vaporized at the same instant the evolved vapors have intimate contact while traveling the same upward circuitous route. This circulation feature not only contributes to maximum reflux but also increases the time element, a very important feature to pro- This prolonged scrubbing and repeated raising and lowering the temperature of the reflux afford favorable conditions to promote cracking.

The problem of good coke making is one and the same as making good cracked distillate and gas products, because, when the best coke is made, the best distillate and gas also result. The most desirable contributing influence to accomplish these two results is low temperature coking. The most perfect control of temperature is with electric heated coking zones. That of course is the reason for employing this type of unit. At the same time, when a heat interchange is employed such as I have displayed and this interchange of heat is sufiicient to approximate what is required, the amount of electrical energy necessary to maintain a desirable heating condition :is negligible.

To successfully produce coke in the manner 'I have displayed requires very selective temperature control andcareful manipulation of the mechanical follow-up. The very fact that it is possible to take enough vapor from the residue in the upper chamber to reduce it to a spongy semisolid paste still able to flow into cylinders is evidence enough that low temperature coking is accomplished, and that a keen selection and gradation of temperature is prevalent throughout this area. On the'other hand, while the heat from hot gases below extracts the volatile portion from the residue as it moves along, the very fact that the temperature of the residue is not allowed .to'take a sudden drop, even for a moment, while in this physical state, is the main determining factor that makes the coking possible,

nd does not let the residue set solid before passing to the coking area below.

In regard to gas and cracked distillateas the quality and texture of the coke is bettered, the characteristics of the gas and cracked distillate are improved. In lowering the coking temperature to accomplish this, the possible percentage of cracked distillate available to be recovered is increased. 'This in turn will increase the B. t. u. value per cu. ft. of the non-condensilo'le gas, when the cracked distillate is removed.

At this point I desire to stress the importance of maintaining a low temperature in producing coke. It is well to appreciate that it is absolutely essential to avoid any marked degree of hydrogenation of coal in the reactions to accomplis'h this. To illustrate, to accomplish favorable hydrogenation of coal requires excessive temperature and pressure. At the same time high temperature coking destroys its texture and high pressure is mechanically difficult.

I propose to carry as low a temperature as is feasible to get good results and have organized a selected temperature control apparatus to accomplish this. For example, the coke will hardly ever reach a temperature of 2009" 'F. in passing through the hottest area. As the low extreme it is necessary to keep above 1200" F. to dissociate the steam.

As a means to this end, I have employed a fluid, such as steam, fed from an outside source, as a dilutent medium in the coking zone, both to control restricted combustion in this area as well as to lower the temperature intensity. I selected steam for this purpose because it has a high specific heat factor and it is the most economical and efiicient. In addition, after its duties-are completed in the coking chamber later in the still, it can still be embodied in the release gas produced, as an asset, and compensate in that way for the amount of heat expended to cause its dissociation.

As stated before, the steam is admitted at the coking area to better control the temperature at this point and as a tempering medium to .control the temperature intensity of the heat, and, as above mentioned, maintain the latter between 1200 F. and 2000 F. In doing this the'steam is absorbing a large quantity of heat. Thus it stores a large reserve of heat and acts as an accumulator. The ratio of steam to air admitted can be regulated to maintain this condition in the combustion zone and the volume of steam and air admitted can be regulated to best suit the reactions in the still, which are equally important.

As the coking temperature is carried. comparatively low, the temperature of the evolved vapor and gas from the coking chamber is very little above the temperature at which the condensible portion will break up to lower boiling compounds under the proper manipulation and association with other vapor. This has been identified as the critical temperature. As long as the vapors do not pass below this temperature the conversion to lower boiling points is still a possibility. Enough time must elapse to allow this conversion to take place. It must be remembered. that this critical temperature is a variable quantity, and is lowered as the complexity of the mass of hydrocarbons involved is broken up and simplified. Thus, if conversion can be set in motion and the vapor be lowered in temperature at the proper rate, this conversion will continue as long as the vapor does not drop below the critical temperature corresponding to the complexity of the mass at that moment. This emphasizes the importance of the time element in successful cracking. 1

This demonstrates the purpose of introducing the steam. I have employed additional means to get the desired result. This is the use of catalytic contact bodies. As the mass of gas,

' vapor, and steam leave 'the coking chamber,

they must pass through the stack of containers in the scrubber. These arefilled with catalytic contact bodies. Fullers earth may be used or iron oxide or a mixture of the two. The latter is very desirable because the iron oxide in addition to encouraging catalytic activity has an afiinity for undesirable components, particularly sulphur and will not let these pass. Thus it acts as a cleanser as well.

As this mass of vapor is moving upward I through the scrubber and then within the heating plates of the still, very important coordinations are being accomplished. Theraw material flowing downwardly over these same plates is absorbing a large quantity of heat from the steam and vapor traveling upward in countercurrent fashion. It is very important, of course, for the raw material to do this to accomplish distillation. On the other hand, it is equally important for the gas, steam and vapor to supply this heat and at the same time to take advantage of the opportunity of being lowered in temperature in gradual and regular fashion. Thus the volume of steam and air admitted to the coking chamber can control this at will. This, of course, keeps the vapor from falling below the critical temperature.

The steam content not only serves this purpose within the heating plates but later after diifusion takes place in the still, and even all the way to the top of the dephlegmator. Thus the time factor is controlled at will and this element is a very important contributing influence in successful cracking. In addition, all the vapor and steam from the coking chamber are diffused with the vapors produced in the still through containers filled with catalytic contact bodies. This association of vapor from two sources and affording intimate contact in a reaction zone in the presence of catalytic contact bodies is favorable to promote cracking and these influences are present all the way to the top of the dephlegmator.

This elaborate manipulation is necessary because coal is the material treated, or broadly speaking, a group of hydrocarbons found as a solid, and when subjected to destructive distillation, hardly half can be recovered as liquid and gas, and the balance will be coke.

With such an abundance of carbon present, the tendency is for liquid hydrocarbons to form that contain a low hydrogen content as for example, the aromatic group. Some of the arcmatic compounds are desirable while others are not. Thus, with liquids forming that contain 100 a low hydrogen content, the loss of free hydrogen escaping and eventually going to the release gas is keenly felt. This results from insufiicient. molecular activity.

This is the purpose of the dissociated steam and catalytic contact bodies to stimulate this activity as well as the other duties listed above. All of these can be coordinated to the best advantage with the employment of pressure and this means stimulatesthe greatest molecular activity.v Mechanical difficulties establishes the. present limit. I would not propose using a pressure in the distilling and coking zone in excess of 300 pounds per square inch gage pressure.

The percentage of coke that should be produced from any particular kind of coalis a variable quantity. This can only be arrived at by actual operating conditions. To follow through v and get the best results fromvany grade of coal requires a well balanced organization of flexible apparatus.

This feature of flexibility is the key-note in' favor ofthis type of apparatus. The temperature can be controlled to such close range that the percentage of coke produced can be regulated to suit the coal employed with the main object as the best grade of coke. The quality of .the gas and cracked distillate products is immediately improved. The admission and equal dis tribution of air and steam are additional features of flexibility that cannot be employed in the old way.

In addition, all of the above desirables can be accomplished and petroleum oil, coal tar or water gas tar may be added to the mixture that is charged, without disturbing the equilibrium in the coking chamber, and at the same time, accomplish desirable cracking results in the balance of the apparatus. a

I claim 1. A contino V method of low temperature coal distillation, which consists in mixing pow- V dered coal with a high boiling liquid hydrocarbon, moving the mixture in an unconfined state in the form of a thin film, and appying heat to said film by conduction while in motion 'to drive ofi volatile constituents therefrom.

2. Ina continuous method of low temperature coaldistillation, the steps which consist in 'mix- 150 in the form of a plurality of simultaneously flowingpowdered coal with aliquid vehicle in a suitable mixing tank, thoroughly stirring the mixture in said tank, passing the mixture through a still in an unconfined state in the form of a thin film to vaporize volatile constituents thereof, passing the evolved vapors through a dephlegmator and scrubbing the same therein, and returning the reflux from said dephlegmator to said mixing tank.

3. In a method of distillation, the steps which consist of passing a feed stock comprising a hydrocarbon through a still in an unconfined state in the form of a plurality of simultaneously flowing thin uni-directional films, simultaneously vaporizing said films under equal heat and pressure,v and causing the vapors from said films to mingle with each other.

4. In a method of distillation, the steps which consist of passing a feed stock comprising a hydrocarbon through a still in an unconfined state ing thin uni-directional films, simultaneously vaporizing said films under equal heat and pressure, causing the vapors from said films to mingle with each other, and then scrubbing and condensing the commingled vapors.

5. A continuous method of producing coke, which consists in mixing powdered coal with a high boiling liquid hydrocarbon, distilling the mixture to vaporize the bulk of the volatile constituents, briquetting the residuum while in a heated and plastic state, and subjecting the residuum during the briquetting thereof to partial combustion to expel the remaining volatile constituents and form coke.

6. A continuous method of producing coke and liquid hydrocarbons, which consists in mixing powdered coal with a high boiling liquid hydrocarbon, passing the mixture through a still to vaporize the bulk of the volatile constituents, briquetting the heated and plastic residuum from the still, subjecting the residuum during the briquetting operation to restricted combustion to expel the remaining volatile constituents and form coke, and passing the hot vapors and gases resulting from such restricted combustion through the still to heat and partially vaporize the mixture flowing through the latter.

7. A continuous method of producing coke and liquid hydrocarbons, which consists in mixing powdered coal with a high boiling liquid hydrocarbon, passing the mixture through a condenser and then through a still to vaporize the bulk of the volatile constituents, briquetting the residuum while in a heated and plastic state, subjecting the residuum during the briquetting operation to restricted combustion to expel the remaining volatile constituents and form coke, passing the hot vapors and gases resulting from such restricted combustion through the still to heat and partially vaporize the mixture flowing through the latter, and then passing said hot vapors and gases mixed with those generated in the still through said condenser out of contact with the infiowing mixture to heat the latter.

8. A continuous method of producing coke and liquid hydrocarbons, which consists in mixing powdered coal with a high boiling liquid hydrocarbon, passing the mixture through a dephlegmator and then through a still to vaporize the bulk of the volatile constituents briquetting the residuum while in a heated and plastic state, subjecting the residuum during the briquetting operation and while under pressure greater than atmospheric to restricted combustion to expel the remaining volatile constituents and form coke, passing the,

hot vapors and gases resulting from such restricted combustion through the still to heat and partially vaporize the mixture flowing through the latter, then passing said hot vapors and gases mixed with those generated in the still through said dephlegmator out of contact with the inflowing mixture to heat the latter, and finally condensing the vapors from said dephlegmator.

9. A continuous method of producing coke and liquid hydrocarbon, which consists in mixing powdered coal with a high boiling liquid hydrocarbon, passing the mixture through a condenser and a dephlegmator and then through a still to vaporize the bulk of the volatile constituents, briquetting the residuum while in a heated and plastic state, subjecting the residuum during the briquetting operation and while under pressure greater than atmospheric to restricted combustion to expel the remaining volatile constituents and form coke, passing the hot vapors and gases resulting from such restricted combustion through the still to heat and partially vaporize the mixture flowing through the latter, and then passing said hot vapors and gases mixed with those generated in the still first through said dephlegmator and then through said condenser out of contact with the infiowing mixture to heat the latter.

10. A continuous method of producing coke and liquid hydrocarbons, which consists in thoroughly commingling powdered coal and a. high boiling liquid hydrocarbon in a suitable mixing chamber, passing the mixture through a dephlegmator and then through a still to vaporize the bulk of the volatile constituents, briquetting the residuum while in a-heated and plastic state, subjecting the residuum during the briquetting operation and while under pressure greater than atmospheric to restricted combustion to expel the remaining volatile constituents and form coke, passing the hot vapors and gases resulting from .such restricted combustion through the still to heat and partially vaporize the mixture flowing through the latter, then passing said hot vapors and gases mixed with those generated in the still through said dephlegmator out of contact with the infiowing mixture, and returning the reflux from said dephlegmator to the feed stock mixture.

11. A continuous method of producing coke and 3% the volatile constituents, passing the residuum from the still into a coking chamber, briquetting the residuum while in a heated andplast-ic state dephlegmator and a still-to vaporize the bulk of U in said coking chamber, subjecting the residuum during the briquetting operation and while under pressure greater than atmospheric to restricted combustion to expel the remaining volatile constituents and form coke, passing the hot vapors and gases resulting from such restricted combus tion through the still to heat and partially vaporize the mixture flowing through the latter, passing said hot vapors and gases mixed with those generated in the still through said dephlegmator and then through saidcondenser out of contact with the infiowing mixture to heat the latter, and returning the reflux from said dephlegmator to the feed stock mixture.

FRANCIS M. HESS. 

